Process for producing exhaust-gases-purifying catalyst

Abstract: A process for producing an exhaust-gases-purifying catalyst includes the steps of loading an NO x adsorbent on a porous support, carbonating the porous support with the NO x adsorbent loaded, thereby converting the NO x adsorbent into carbonate, and loading a noble metal catalyst ingredient on the porous support with the carbonate loaded. The process can produce an exhaust-gases-purifying catalyst on which the NO x adsorbent and the noble metal catalyst ingredient are loaded in large amounts and which can stably and efficiently purify NO x during the fuel-lean side (i.e., in the oxygen-rich atmospheres) driving.

Description: The present invention relates to a process for producing an exhaust-gases-purifying catalyst. More particularly, it relates to a process for producing an exhaust-gases-purifying catalyst which can efficiently purify nitrogen oxides (NO X ) in exhaust gases whose oxygen concentrations are at the stoichiometric point or more than required for oxidizing carbon monoxide (CO) and hydrocarbons (HC) therein. As catalysts for purifying automotive exhaust gases, there have been employed 3-way catalysts so far which oxidize CO and RC and reduce NO X to purify the exhaust gases. For example, the 3-way catalysts have been known widely which comprise a heat resistant support formed of cordierite, a catalyst carrier layer formed of gamma-alumina and disposed on the support, and a noble metal catalyst ingredient selected from the group consisting of Pt, Pd and Rh and loaded on the catalyst carrier layer. The purifying performance of the 3-way catalysts for purifying exhaust gases depends greatly on the air-fuel ratio A/F of automotive engine. For instance, when the air-fuel weight ratio is larger than 14.6, i.e., when the fuel concentration is low (or on the fuel-lean side), the oxygen concentration is high in exhaust gases. Accordingly, the oxidation reactions purifying CO and HC are active, but the reduction reactions purifying NO X are inactive. On the other hand, when the air-fuel ratio is smaller than 14.6, i.e., when the fuel concentration is higher (or on the fuel-rich side), the oxygen concentration is low in exhaust gases. Accordingly, the oxidation reactions are inactive, but the reduction reactions are active. From document DE 38 32 268 a process for manufacturing a catalyst is known, wherein gold as the noble metal compound is loaded on the surface of alkaline-earth metal compounds. In this respect, it has been suggested to contact carbonate particles carried on a support with a gold solution. Thus, the alkaline-earth metal compounds act as a carrier for the gold particles. Moreover, the alkaline-earth metal compounds should have a low solubility in water. From document JP-A-60 206 448 it has become known to deposit a carbonated NOx-adsorbing compound on a support and to subsequently deposit a noble metal from a solution. The noble metal is loaded on a support comprising NO 2 -interstitial lanthanum oxide (La 2 O 3 •CO 2 ) and alumina, wherein the NO 2 -interstitial lanthanum oxide (La 2 O 3 .CO 2 ) is a powder. When the noble metal is loaded in an aqueous solution condition on the support comprising NO 2 -interstitial lanthanum oxide (La 2 O 3 •CO 2 )and alumina, due to the difference of adsorbability between NO 2 -interstitial lanthanum oxide (La 2 O 3 •CO 2 ) and alumina, the noble metal is mainly loaded on alumina, and it is hardly loaded on NO 2 - interstitial lanthanum oxide (La 2 O 3 •CO 2 ). Accordingly, NO 2 -interstitlal lanthanum oxide (La 2 O 3 •CO 2 ) is not adjacent to the noble metal. Moreover, when driving automobiles, especially when driving automobiles in urban areas, the automobiles are accelerated and decelerated frequently. Consequently, the air-fuel ratio varies frequently in the range of from the values adjacent to the stoichiometric point (or the theoretical air-fuel ratio: 14.6) to the fuel-rich side. In order to satisfy the low fuel consumption requirement during the driving conditions such as in the above-described urban areas, it is necessary to operate the automobiles on the fuel-lean side where the air-fuel mixture containing oxygen as excessive as possible is supplied to the engines. Hence, it has been desired to develop a catalyst which is capable of adequately purifying NO X even on the fuel-lean side (i.e., in the oxygen-rich atmospheres). In view of the aforementioned circumstances, the applicant of the present invention and others applied for a Japanese Patent for a novel catalyst under Japanese Patent Application No. 4-130,904 (Japanese Unexamined Patent Publication (KOKAI) No. 5-317,652. On this catalyst, there are loaded an alkaline-earth metal oxide and Pt. On the catalyst, for example, barium is loaded in the form of its simple oxide. In the catalyst, during the fuel-lean side (i.e., in the oxygen-rich atmospheres) driving, when the catalyst acts as a NO X - absorbent, the simple oxide reacts with NO X to form alkaline-earth metal nitrate (e.g., barium nitrate (Ba(NO 3 ) 2 ), and the alkaline-earth metal nitrate reacts with the reducing gas such as HC and the like to be purified. As a result, the catalyst exhibits superb NO X purifying performance during the fuel-lean side (i.e., in the oxygen-rich atmospheres) driving. Japanese Unexamined Patent Publication (KOKAI) No. 5-317,652 also sets forth a process for producing the catalyst. That is, an active alumina coating layer is formed on a support made from cordierite or the like, and Pt is loaded on the coating layer by an ordinary method. Thereafter, the coating layer is impregnated with an aqueous solution of barium acetate or the like, dried and calcinated to load Ba or the like thereon. However, in the case where Pt is loaded, and thereafter Ba or the like is loaded, Pt is covered with Ba or the like. Accordingly, Pt might not be able to fully exhibit its inherent functions. Namely, the catalyst might not be able to sufficiently exhibit its NO oxidation action and its NO 2 reduction action. As a result, there arises a problem in that the catalyst might exhibit deteriorated NO x conversion which is lower than expected NO x conversion. Hence, one can think of first loading Ba or the like and then loading Pt. However, this process might result in a problem in that Ba or the like, loaded on purpose, elutes into an aqueous solution for loading Pt. When loaded Ba or the like elutes into an aqueous solution of Pt compound, not only the loading amount of Ba or the like might be decreased, but also Pt might be eventually precipitated and deposited by variation of the pH value in the aqueous solution. As a result, the loading amount of Pt might be decreased. The present invention has been developed in view of the aforementioned circumstances. It is therefore an object of the present invention to provide a process for producing an exhaust-gases-purifying catalyst which enables to finally load noble metal catalyst ingredient, which enables to inhibit an NO X adsorbent such as Ba or the like from eluting, and which enables to load the NO X adsorbent and the noble metal catalyst ingredient in large amounts. This object is achieved by the process for producing an exhaust-gases-purifying catalyst according to claim 1. As for the porous support, it is possible to employ a honeycomb support made from cordierite, a honeycomb support coated with an active alumina coating layer, and a honeycomb support made from heat resistant metal and coated with an active alumina coating layer. As for alkaline-earth metal element constituting the alkaline-earth metal compound, it is possible to employ at least one element selected from the group consisting of Mg, Ca, Sr, Ba and Ra, and it is especially preferable to employ at least one element selected from the group consisting of Ba and Sr. Moreover, in the step of loading NO X adsorbent, it is preferable to load the NO X adsorbent on the porous support in an amount of from 0.05 to 1.0 mole with respect to 1 liter of the porous support. As for the carbonating, the following methods are available: bringing the porous support, with the NO X adsorbent loaded, into contact with an aqueous solution of carbonic acid, bringing the support into contact with an aqueous solution of ammonium carbonate, and bringing the support into contact with a CO 2 gas. When bringing the support into contact with the carbonic acid aqueous solution or the ammonium carbonate aqueous solution, it is preferable to saturate the aqueous solution and use the saturated aqueous solution. When bringing the support into contact with the CO 2 gas, it is preferable to use the CO 2 gas having a CO 2 concentration of 10% by volume or more and to bring the support into contact with the CO 2 gas which is heated to a temperature of from 100 to 650 °C. It is also possible to heat the support to the temperature and bring it into contact with the CO 2 gas. Further, in the step of carbonating, it is preferable to bring the support into contact with the aqueous solution of carbonic acid at room temperature for a period of from 0.5 to 5 hours. Furthermore, in the step of carbonating, it is preferable to bring the support into contact with the aqueous solution of ammonium carbonate at room temperature for a period of from 0.5 to 50 hours. Moreover, in the step of carbonating, it is preferable to bring the support into contact with the CO 2 gas at the temperature of from 100 to 650 °C for a period of from 0.5 and 48 hours. As for the noble metal catalyst ingredient, it is possible to employ at least one element selected from the group consisting of Pt, Pd and Rh. Moreover, it is preferable to load the noble metal catalyst ingredient on the porous support in an amount of from 0.1 to 10 grams with respect to 1 liter of the porous support. In the present process for producing an exhaust-gases-purifying catalyst, the NO X adsorbent is first loaded on the porous support in the NO X adsorbent loading step, and it is carbonated in the carbonating step. Thus, the NO X adsorbent is converted into carbonate, and it is now insoluble or difficult to dissolve into an aqueous solution of a noble metal catalyst ingredient which is used in the subsequent noble metal catalyst ingredient loading step. As a result, when the porous support is immersed into an aqueous solution of a noble metal catalyst ingredient in the subsequent loading step, the NO X adsorbent can be inhibited from eluting into the aqueous solution. Hence, the loading amount of the NO X loaded in the NO X adsorbent loading step hardly varies, and accordingly initial high NO X adsorbent loading can be maintained. Moreover, since the NO X adsorbent scarcely elutes, the pH little varies in the aqueous solution of a noble metal catalyst ingredient. Consequently, the noble metal catalyst ingredient can be inhibited from precipitating and depositing. Thus, in the noble metal catalyst ingredient loading step, the noble metal catalyst ingredient can be loaded in a large amount. In particular, the NO X adsorbent is loaded, and thereafter the noble metal catalyst ingredient is loaded. Therefore, there scarcely arises the problem in that the noble metal catalyst ingredient is covered with the NO X adsorbent, and accordingly the catalytic actions of the noble metal catalyst ingredient can be maximized. In accordance with the present process for producing an exhaust-gases-purifying catalyst, the NO X adsorbent and the noble metal catalyst ingredient can be loaded in large amounts, respectively. Hence, an exhaust-gases-purifying catalyst produced in accordance with the present process can be maximized in terms of the NO X adsorbing action resulting from the NO X adsorbent as well as the oxidation and reduction actions resulting from the noble metal catalyst ingredient. Further, the catalyst can exhibit favorable NO X purifying performance even after a durability test. Furthermore, the catalyst can stably and efficiently purify NO X during the fuel-lean side (i.e., in the oxygen-rich atmospheres) driving. DETAILED DESCRIPTION OF THE PREFERRED EMBODIMENTS Having generally described the present invention, a further understanding can be obtained by reference to the specific preferred embodiments which are provided herein for purposes of illustration only and are not intended to limit the scope of the appended claims. Unless otherwise specified, the term, "parts," hereinafter means "parts by weight." First Preferred Embodiment 100 parts of an alumina powder, 70 parts of alumina sol containing alumina in an amount of 10% by weight, 15 parts of an aqueous aluminum nitrate solution containing aluminum nitrate in an amount of 40% by weight, and 30 parts of water were mixed, thereby preparing a slurry for coating. Then, a plurality of honeycomb supports formed of cordierite were immersed into the slurry, and thereafter each of them was blown to blow away the slurry in excess. Each of the supports was dried, and thereafter each of them was calcinated at 600 °C for 1 hour, thereby forming an alumina coating layer thereon. The alumina coating layer was thus coated on the honeycomb support in an amount of 120 grams with respect to 1 liter of the honeycomb support. (NO X Adsorbent Loading Step) Each of the honeycomb supports having the alumina coating layer thereon was immersed into a mixed aqueous solution of barium acetate and lithium nitrate, and thereafter each of them was blown to blow away the water droplets in excess. Each of the supports was dried at 120 °C, and each of them was calcinated at 500 °C for 1 hour, thereby loading Ba and Li thereon. The Ba was thus loaded thereon in an amount of 0.3 moles with respect to 1 liter of the honeycomb support. The Li was thus loaded thereon in an amount of 0.1 mole with respect to 1 liter of the honeycomb support. When this step is completed, the Ba and Li were loaded thereon as its hydroxide and oxide, respectively. That is, the Ba and Li in the form of its hydroxide and oxide were likely to elute into an aqueous solution of a noble metal catalyst ingredient later described. (Carbonating Step) In order to overcome the aforementioned drawback, each of the honeycomb supports with the Ba and Li loaded was immersed into a saturated carbonic acid aqueous solution at ordinary temperature for 1 hour. After taking each of the supports out of the saturated carbonic acid aqueous solution, each of them was dried at 120 °C. Thus, the Ba and Li were converted into their insoluble carbonates, e.g., BaCO 3 and Li 2 CO 3 , respectively. (Noble Metal Catalyst Ingredient Loading Step) Each of the honeycomb supports undergone up to the carbonating step, each of them was immersed into an aqueous platinum dinitrodiammine solution having a predetermined concentration, and thereafter it was blown to blow away the water droplets in excess. After the blowing, each of the supports was dried, and each of them was calcinated at 250 °C for 1 hour, thereby loading Pt thereon. The loading amount of Pt was 2.0 grams with respect to 1 liter of the honeycomb support. Moreover, each of the honeycomb supports with the Pt loaded was immersed into an aqueous rhodium chloride solution having a predetermined concentration, and thereafter each of them was blown to blow away the water droplets in excess. After the blowing, each of the supports was dried, and each of them was calcinated at 250 °C for 1 hour, thereby loading Rh thereon. The loading amount of Rh was 0.1 grams with respect to 1 liter of the honeycomb support. During the noble metal catalyst ingredient loading step, the Ba and Li were loaded as their carbonates, and accordingly they hardly eluted into the aqueous platinum dinitrodiammine solution and into the aqueous rhodium chloride solution. As a result, during this loading step, their initial loading amounts could be maintained. Moreover, since they hardly eluted into the aqueous solutions, the pH values scarcely varied in the aqueous solutions so that the Pt and Rh little precipitated. In addition, during the noble metal catalyst ingredient loading step, loading rates of the Pt and Rh were derived from the variations between the concentrations of the aqueous platinum dinitrodiammine solution and the aqueous rhodium chloride solution before and after the noble metal catalyst ingredient loading step. Moreover, elution rates of the Ba and Li were derived from the concentrations of the Ba and Li in the aqueous solutions after the noble metal catalyst ingredient loading step. The thus derived loading rates and elution rates are summarized in Table 1 below. Second Preferred Embodiment Except that, in the carbonating step, a 1N ammonium carbonate aqueous solution was used, the Second Preferred Embodiment of the present process was carried out in the same manner as the First Preferred Embodiment. Namely, in the carbonating step, each of the honeycomb supports with the Ba and Li loaded was immersed into and processed in the ammonium carbonate aqueous solution, instead of the saturated carbonic acid aqueous solution, at ordinary temperature for 1 hour. Third Preferred Embodiment Except that, in the carbonating step, each of the honeycomb supports with the Ba and Li loaded was processed in a CO 2 gas atmosphere heated to 300 °C, instead of immersing it into the saturated carbonic acid aqueous solution, for 1 hour, the Third Preferred Embodiment of the present process was carried out in the same manner as the First Preferred Embodiment. Comparative Example No. 1 Except that the noble metal catalyst ingredient loading step was carried out subsequent to the NO X adsorbent loading step, Comparative Example No. 1 was carried out in the same manner as the First Preferred Embodiment. Comparative Example No. 2 Except that the noble metal catalyst ingredient loading step was first carried out, thereafter the NO X adsorbent loading step was carried out, and no carbonating step was carried out, Comparative Example No. 2 was carried out in the same manner as the First Preferred Embodiment. Fourth Preferred Embodiment Except that, in the NO X adsorbent loading step, no lithium nitrate aqueous solution was used to load Ba only, the Fourth Preferred Embodiment of the present process was carried out in the same manner as the First Preferred Embodiment. Comparative Example No. 3 Except that, in the NO X adsorbent loading step, no lithium nitrate aqueous solution was used to load Ba only, and the noble metal catalyst ingredient loading step was carried out subsequent to the NO X adsorbent loading step without being intervened by the carbonating step, Comparative Example No. 3 was carried out in the same manner as the First Preferred Embodiment. Comparative Example No. 4 Except that the noble metal catalyst ingredient loading step was first carried out to load the noble metal catalyst ingredients, and, in the NO X adsorbent loading step, no lithium nitrate aqueous solution was used to load Ba only, and no carbonating step was carried out, Comparative Example No. 4 was carried out in the same manner as the First Preferred Embodiment. Fifth Preferred Embodiment Except that, in the NO X adsorbent loading step, no lithium nitrate aqueous solution was used, and, instead of the barium acetate aqueous solution, a strontium acetate aqueous solution was used to load Sr in the same loading amount, the Fifth Preferred Embodiment of the present process was carried out in the same manner as the First Preferred Embodiment. Comparative Example No. 5 Except that, in the NO X adsorbent loading step, no lithium nitrate aqueous solution was used, and, instead of the barium acetate aqueous solution, a strontium acetate aqueous solution was used to load Sr, and the noble metal catalyst ingredient loading step was carried out subsequent to the NO X adsorbent loading step without being intervened by the carbonating step, Comparative Example No. 5 was carried out in the same manner as the First Preferred Embodiment. Comparative Example No. 6 Except that the noble metal catalyst ingredient loading step was first carried out to load the noble metal catalyst ingredients, and, in the NO X adsorbent loading step, no lithium nitrate aqueous solution was used, and, instead of the barium acetate aqueous solution, a strontium acetate aqueous solution was used to load Sr, and no carbonating step was carried out, Comparative Example No. 5 was carried out in the same manner as the First Preferred Embodiment. Sixth Preferred Embodiment Except that, in the NO X adsorbent loading step, no lithium nitrate aqueous solution was used, and, instead of the barium acetate aqueous solution, a calcium acetate aqueous solution was used to load Ca in the same loading amount, the Sixth Preferred Embodiment of the present process was carried out in the same manner as the First Preferred Embodiment. Comparative Example No. 7 Except that, in the NO X adsorbent loading step, no lithium nitrate aqueous solution was used, and, instead of the barium acetate aqueous solution, a calcium acetate aqueous solution was used to load Ca, and the noble metal catalyst ingredient loading step was carried out subsequent to the NO X adsorbent loading step without being intervened by the carbonating step, Comparative Example No. 7 was carried out in the same manner as the First Preferred Embodiment. Comparative Example No. 8 Except that the noble metal catalyst ingredient loading step was first carried out to load the noble metal catalyst ingredients, and, in the NO X adsorbent loading step, no lithium nitrate aqueous solution was used, and, instead of the barium acetate aqueous solution, a calcium acetate aqueous solution was used to load Ca, and no carbonating step was carried out, Comparative Example No. 8 was carried out in the same manner as the First Preferred Embodiment. Seventh Preferred Embodiment Except that, in the NO X adsorbent loading step, no lithium nitrate aqueous solution was used, and, instead of the barium acetate aqueous solution, a magnesium acetate aqueous solution was used to load Mg in the same loading amount, the Seventh Preferred Embodiment of the present process was carried out in the same manner as the First Preferred Embodiment. Comparative Example No. 9 Except that, in the NO X adsorbent loading step, no lithium nitrate aqueous solution was used, and, instead of the barium acetate aqueous solution, a magnesium acetate aqueous solution was used to load Mg, and the noble metal catalyst ingredient loading step was carried out subsequent to the NO X adsorbent loading step without being intervened by the carbonating step, Comparative Example No. 8 was carried out in the same manner as the First Preferred Embodiment. Comparative Example No. 10 Except that the noble metal catalyst ingredient loading step was first carried out to load the noble metal catalyst ingredients, and, in the NO X adsorbent loading step, no lithium nitrate aqueous solution was used, and, instead of the barium acetate aqueous solution, a magnesium acetate aqueous solution was used to load Mg, and no carbonating step was carried out, Comparative Example No. 10 was carried out in the same manner as the First Preferred Embodiment. Examination and Evaluation Each of the catalysts produced by the First through Seventh Preferred Embodiments and Comparative Example Nos. 1 through 10 was disposed in an exhaust line of an actual vehicle equipped with a lean burn engine. The lean burn engine had a displacement of 1.6 liters. The vehicle was driven in the urban area running mode, for instance, it was alternately driven in the 10-mode for a certain period of time and then in the 15-mode for another certain period of time, thereby examining the catalysts for the conversion of NO X . The results of the examination are summarized in the column designated at "Initial NO X Conversion" in Table 1. After the aforementioned evaluation, each of the catalysts produced by the First through Seventh Preferred Embodiments and Comparative Example Nos. 1 through 10 was subjected to a bench test on durability which utilized the same type of engine as above. Namely, each of them was disposed in an exhaust line of the engine, and then the engine was run for 50 hours while adjusting the temperature of the exhaust gas introduced into them at 650 °C at an air-fuel ratio A/F of 18. After this bench test was over, each of them was again disposed in the exhaust line of the actual vehicle. The vehicle was driven in the same manner as described above, thereby examining the catalysts for the conversion of NO X . The results of the examination are summarized in the column designated at "NO X Conversion after Durability Test" in Table 1. In addition, during the noble metal catalyst ingredient loading step, loading rates of the Pt and Rh were derived from the variations between the concentrations of the Pt and Rh in the aqueous platinum dinitrodiammine solution and the aqueous rhodium chloride solution before and after the noble metal catalyst ingredient loading step. Moreover, elution rates of the Ba, Li, Sr, Ca and Mg were derived from the concentrations of the Ba, Li, Sr, Ca and Mg in the aqueous solutions after the noble metal catalyst ingredient loading step. The thus derived loading rates and elution rates are also summarized in Table 1. It is understood from Table 1 that, although the elution rates of the NO X adsorbents were high in Comparative Example Nos. 1, 3, 5, 7 and 9 in which no carbonating step was carried, the elution rates were controlled to be low in the First through Seventh Preferred Embodiments of the present process. As a result, in the First through Seventh Preferred Embodiments of the present process, the noble metal catalyst ingredients were inhibited from precipitating and depositing, and their loading rates were kept high. That is, both of the NO X adsorbents and the noble metal catalyst ingredients were loaded in higher loading amounts by the First through Seventh Preferred Embodiments of the present process than by Comparative Example Nos. 1, 3, 5, 7 and 9. As a result, the catalysts produced by the First through Seventh Preferred Embodiments of the present process were apparently improved in terms of the initial NO X conversion and the NO X conversion after a durability test. Since the noble metal catalyst ingredients were first loaded and thereafter the NO X adsorbents were loaded by Comparative Example Nos. 2, 4, 6, 8 and 10, the loading rates of the noble metal catalyst ingredients were high and the catalysts produced by Comparative Example Nos. 2, 4, 6, 8 and 10 exhibited high loading rates of the noble metal catalyst ingredients as well as high initial NO X conversion. However, the catalysts produced by Comparative Example Nos. 2, 4, 6, 8 and 10 were inferior to the catalysts produced by the First through Seventh Preferred Embodiments of the present process in terms of the NO X conversion after a durability test. This disadvantageous effect is believed to result from the phenomenon that, in Comparative Example Nos. 2, 4, 6, 8 and 10, the novel metal catalyst ingredients were covered up with the. NO X adsorbents as time elapsed, and that they could not fully effect their activity.

Claims: A process for producing an exhaust-gases-purifying catalyst, comprising the steps of: loading at least one metallic compound selected from the group consisting of Li and alkaline-earth metal compound on a porous support as an NOx adsorbent which can be carbonated for inhibiting elution of said NOx adsorbent by using an aqueous solution in which said NOx adsorbent is dissolved; carbonating said porous support with said NOx adsorbent loaded, thereby converting said NOx adsorbent into carbonate which enables to inhibit said NOx adsorbent from eluting in a subsequent step; and loading a noble metal catalyst ingredient from an aqueous solution on said porous support with said carbonate loaded. The process according to Claim 1, wherein said step of loading NO X adsorbent is carried out so as to load said NO X adsorbent on said porous support in an amount of from 0.05 to 1.0 mole with respect to 1 liter of said porous support. The process according to Claim 1, wherein said step of carbonating is carried out by bringing said porous support, with said NO X adsorbent loaded, into contact with an aqueous solution of carbonic acid. The process according to Claim 3, wherein said step of carbonating is carried out by using a saturated aqueous solution of carbonic acid. The process according to Claim 3, wherein said step of carbonating is carried out at a predetermined temperature for a predetermined period of time, which is effective to convert said NO X adsorbent into its insoluble carbonate. The process according to Claim 5, wherein said step of carbonating is carried out at room temperature for a period of from 0.5 to 5 hours. The process according to Claim 1, wherein said step of carbonating is carried out by bringing said porous support, with said NO X adsorbent loaded, into contact with an aqueous solution of ammonium carbonate. The process according to Claim 7, wherein said step of carbonating is carried out by using a saturated aqueous solution of ammonium carbonate. The process according to Claim 7, wherein said step of carbonating is carried out at a predetermined temperature for a predetermined period of time, which is effective to convert said NO X adsorbent into its insoluble carbonate. The process according to Claim 9, wherein said step of carbonating is carried out at room temperature for a period of from 0.5 to 5 hours. The process according to Claim 1, wherein said step of carbonating is carried out by bringing said porous support, with said NO X adsorbent loaded, into contact with a CO 2 gas. The process according to Claim 11, wherein said step of carbonating is carried out by using said CO 2 gas having a CO 2 concentration of 10% by volume or more. The process according to Claim 11, wherein said step of carbonating is carried out at a predetermined temperature for a predetermined period of time, which is effective to convert said NO X adsorbent into its insoluble carbonate. The process according to Claim 13, wherein said step of carbonating is carried out at a temperature of from 100 to 650 °C for a period of from 0.5 and 48 hours. The process according to Claim 1, wherein said step of loading noble metal catalyst ingredient further includes the step of selecting at least one element from the group consisting of Pt, Pd and Rh. The process according to Claim 1, wherein said step of loading noble metal catalyst ingredient is carried out so as to load said noble metal catalyst ingredient on said porous support in an amount of from 0.1 to 10 grams with respect to 1 liter of said porous support.

Inventors: MURAMOTO RIEMI, MURAMOTO, RIEMI
Applicants: TOYOTA MOTOR CO LTD, TOYOTA JIDOSHA KABUSHIKI KAISHA
Application year: 1994
Main classification: B01D53
IPC codes: B01J23, B01J37, C01B31, B01D53, B01J27